JP2003106699A - Absorption type refrigerator - Google Patents

Abstract

PROBLEM TO BE SOLVED: To reduce a temperature and a pressure in a refrigerating cycle by reducing a margin of concentration of absorption solution in a regenerator on the most low temperature side and a regenerator on the most high temperature side. SOLUTION: In an absorption type refrigerator having the number of n (n>=3) regenerators G1 to Gn, the refrigerating cycle is constituted in such a way that (ξ1 -ξa ) and (ξn -ξa ) are smaller than (ξm -ξa ) when concentration of absorption solution Lcn after refrigerant vapor is generated in the regenerator Gn on the most high temperature side is ξn ; concentration of absorption solution Lc1 after refrigerant vapor is generated in the regenerator G1 on the most low temperature side is ξ1 ; concentration of absorption solution Lc flowing into an absorber A is ξm ; and concentration of absorption solution Lw flowing out from the absorber A is ξa . In this constitution, a temperature and a pressure in the refrigerating cycle are reduced.

Description

Detailed Description of the Invention

[0001]

TECHNICAL FIELD The present invention is n (n ≧ 3).
The present invention relates to an absorption type refrigeration system including the regenerator.

[0002]

2. Description of the Related Art For example, an absorption type refrigerating apparatus having three regenerators is shown in FIGS. The absorption type refrigerating apparatus shown in FIGS. 32 to 34 has a condenser C, an absorber A, an evaporator E and three regenerators G ₁ , G ₂ and G ₃ as basic elements, and a space between these elements is a solution. In the regenerator G ₃ on the high temperature side, the absorbent solution is heated and boiled by using an external heat source J such as fuel or steam to generate a refrigerant vapor R ₃ and the refrigerant vapor R ₃ is generated. by heating the medium-temperature side of the absorption solution regenerator G ₂ is a single stage low temperature side by using the heat of the R ₃ to generate refrigerant vapor R _2, further low-temperature side of the regenerator with the refrigerant vapor R ₂ G While heating the _first absorption solution and is configured to generate a refrigerant vapor R _1, FIG. 3
The flow of the absorbing solution is different between the case of Conventional Example 1 shown in FIG. 2, the case of Conventional Example 2 shown in FIG. 33, and the case of Conventional Example 3 shown in FIG.

That is, in the case of the conventional example 1 shown in FIG. 32, the absorbing solution (dilute solution) Lw having the concentration ξ _a , which has flowed out of the absorber A, is introduced into the regenerator G ₃ on the high temperature side and is concentrated therein. become absorbed solution (concentrated solution) Lc ₃ concentrations xi] ₃ flows into the regenerator G ₃ mesophilic side, the reproduction of the low temperature side where it is concentrated to a absorbing solution (concentrated solution) Lc ₂ concentrations xi] ₂ It flows into the vessel G ₁ and is concentrated there to become an absorbing solution (concentrated solution) Lc ₁ having a concentration ξ ₁ and returns to the absorber A. In the case of Conventional Example 2 shown in FIG. absorption solution having a concentration xi] _a exiting a (dilute solution) Lw flows into the regenerator G ₁ on the low temperature side, where it is enriched concentration xi] ₁ of the absorbent solution (concentrated solution) Lc ₁ and turned by medium temperature side the flows into the regenerator G _2, where it is concentrated to a concentration xi] ₂ absorption solution becomes (concentrated solution) Lc ₂ flows into the regenerator G ₃ on the high temperature side, where it is concentrated Absorption solution of degree ξ ₃ (concentrated solution)
Lc ₃ is returned to absorber A, as shown in FIG.
In the case of the conventional example 3 shown in FIG. 4, the absorbing solution (dilute solution) Lw having the concentration ξ _a exiting the absorber A is the high temperature side regenerator G ₃ , the middle temperature side regenerator G ₂ and the low temperature side regenerator G. ₁ is branched into ₁ and concentrated in each of the regenerators G ₃ , G ₂ and G ₁ to obtain an absorbing solution (concentrated solution) L having a concentration of ξ ₃ , ξ ₂ and ξ ₁ , respectively.
c _3, Lc _2, merges mixed after flowing out becomes Lc ₁ has a return to the absorber A is the absorption solution (concentrated solution) Lc concentrations xi] _m. That is, the flow of the absorbing solution is reversed between the conventional examples 1 and 2, and in the case of the conventional example 3, the absorbing solution is branched and flows in parallel. The state change of the absorbing solution in Conventional Examples 1, 2 and 3 is
This is as shown in the Dühring diagram shown in FIGS. 35 to 37.

[0004]

By the way, in the case of the above-mentioned conventional examples 1 and 2, since the absorbing solution has a cycle in which the solution is not branched, (ξ ₃ −ξ _a ) or (ξ _m −ξ _a ) is either Is equal to (ξ _m −ξ _a ), but in the case of Conventional Example 3, since the absorbing solution has a cycle of branching, the flow rate of the absorbing solution flowing into the high temperature side regenerator G ₃ becomes small. , A solution for preheating the absorbing solution before flowing into the high temperature side regenerator G ₃ (that is, recovering the heat held by the absorbing solution (concentrated solution) flowing out from the high temperature side regenerator G ₃ ) and we can reduce the size of the solution heat exchanger even when using a heat exchanger, from where also decreases sensible heat of absorption solution heated to boiling in the regenerator G ₃ on the high temperature side, the high temperature side to the regenerator G ₃ The heat input amount (that is, the heat input amount from the external heat source J) can be reduced, There is a fact that COP is also good.

On the other hand, the problems of the absorption type refrigerating apparatus having three or more regenerators are that the internal resistance is high,
The temperature of the absorbing solution becomes high, for example, exceeds 200 ° C., and lowering these is an issue in providing a safe and efficient device.

By the way, in the above-mentioned conventional examples 1 to 3,
, The high temperature side regenerator G₃Of fuel, steam, etc.
Refrigerant vapor R by heating and boiling using an external heat source J₃From
Let the refrigerant vapor R₃On the low temperature side using the heat of
Medium temperature regenerator G₂To heat the refrigerant vapor R₂Occurs
And further, the refrigerant vapor R₂Regenerator G on the low temperature side₁
To heat the refrigerant vapor R₁Absorption refrigeration of the type that generates
In the case of equipment, the regenerator G on the low temperature side₁The boiling temperature of the medium temperature side
Regenerator G₂And high temperature side regenerator G₃Occurs in
Regenerator G on the high temperature side, which is lower than the temperature of the refrigerant vapor₃At
In order to lower the temperature of the generated refrigerant vapor,
Organ G₁It is necessary to lower the boiling temperature of. This boiling temperature
To reduce the temperature, the regenerator G on the low temperature side₁Spill from
Concentration of absorbing solution (concentrated solution) ξ₁Need to lower.

On the other hand, as described above, the regenerator G on the high temperature side
_When the temperature of the absorbing solution of ₃ exceeds 200 ° C., particularly in a case where a halide such as lithium bromide (Libr) is a main component of the absorbing solution, the metal corrosiveness also increases. It is necessary to suppress the temperature of the high temperature side regenerator G ₃ , but for that purpose, it is necessary to reduce the concentration ξ ₃ of the absorbing solution (concentrated solution) flowing out from the high temperature side regenerator G ₃ .

The present invention has been made in view of the above points, and the temperature and pressure in the refrigeration cycle are reduced by reducing the concentration range of the absorbing solution in the regenerator on the lowest temperature side and the regenerator on the highest temperature side. The purpose is to be able to lower.

[0009]

According to the invention of claim 1,
As a means for solving the above problems, a condenser C, an absorber
A and evaporator E and n (n ≧ 3) regenerators G₁~ G_nTo
As basic elements, between these elements, solution piping and refrigerant piping
Operatively coupled with the regenerator G on the hottest side_n At
Is heated and boiled using an external heat source J such as fuel or steam
Refrigerant vapor R_nTo generate the refrigerant vapor R_nUsing the heat of
Regenerator G on the 1st-stage low temperature side_n-1To heat the refrigerant vapor R_n-1From
The refrigerant vapor R_n-1Even lower temperature
Side regenerator G_n-2To heat the refrigerant vapor R_n-2Generate
That the regenerator G on the lowest temperature side₁To get up to
In the configured absorption refrigeration system, the highest temperature side
Regenerator G_nAbsorption solution Lc after generation of refrigerant vapor in_nNono
Ξ_n, The regenerator G at the lowest temperature side₁Refrigerant vapor in
Absorbing solution Lc after generation₁The concentration of ξ₁, Flow to the absorber A
The concentration of the absorption solution Lc to enter is ξ_m, Flow from the absorber A
Let ξ be the concentration of the absorption solution Lw_aAnd (ξ₁−ξ
_a) And (ξ_n−ξ_a) And (ξ_m−ξ_a) Smaller than
It constitutes a refrigeration cycle.

With the above configuration, the concentration width (ξ ₁ −ξ _a ) in the regenerator G ₁ on the lowest temperature side and the concentration width (ξ _n −ξ _a ) in the regenerator G _n on the highest temperature side are It becomes smaller than the concentration width (ξ _m −ξ _a ) between the inlet and the outlet of the absorber A, and the temperature and pressure in the refrigeration cycle can be reduced. As a result, it is possible to reduce the cost associated with the reduction of the transportation power and the reduction of the strength of each element constituting the refrigeration cycle, and the corrosion risk can be reduced.

As in the invention of claim 2, claim 1
In the absorption refrigeration system described above, outflow from the absorber A
The absorbed solution Lw is branched, and one of
Regenerator G₁Flow into the
Part of the regenerator G with the highest temperature_n Configured to flow into
Regenerator G on the highest temperature side_nConcentration flowing into ξ_aSucking
The flow rate of the collecting solution (dilute solution) Lw can be reduced.
As a result, the sensible heat content of the heating and boiling absorbing solution Lw decreases. Servant
Therefore, the heat input to the regenerator is reduced, and COP
improves.

As in the invention of claim 3, claim 2
In the absorption refrigeration apparatus described, regeneration of the highest temperature side
Bowl G_nPart of the absorption solution Lw flowing into the
Regenerator G_nAnd the regenerator G at the lowest temperature side₁Provided between
Regenerator G on the medium temperature side₂~ G_n-1At least one or more of
When it is configured to flow into the₂ ~
G_n-1The flow rate of the solution flowing into the regenerator G on the highest temperature side_n
It is possible to reduce the flow rate to the regenerator on the medium temperature side.
G₂~ G_n-1Concentration of concentrated solution exiting₂~ Ξ_n-1Is the hottest side
Regenerator G_nConcentration of concentrated solution exiting_nGet bigger, contract
The effect of Requirement 1 can be easily obtained.

As in the invention of claim 4, claim 2
In the absorption refrigeration system according to any one of 1 and 3, the absorption solution Lc ₁ flowing out from the regenerator G ₁ on the lowest temperature side is the regenerator G _n on the highest temperature side and the regenerator G on the lowest temperature side. The regenerators G _{2 to} G _n-1 on the medium temperature side provided between the regenerators ₁ and _2.
If it is configured to flow into at least one of
The absorption solution (concentrated solution) Lc _{1 of} concentration ξ ₁ flowing out from the regenerator G ₁ on the lowest temperature side was generated in the regenerator G _n on the highest temperature side in the regenerators G _{2 to} G _n-1 on the medium temperature side. is heated to boiling by the heat of the refrigerant vapor R _n, further has a be concentrated, the concentration ξ ₂ ~ξ _n-1 is the lowest temperature side of the concentrated solution leaving the regenerator G ₂ ~G _n-1 of the medium-temperature side The concentration is larger than the concentration ξ ₁ of the concentrated solution exiting the regenerator G _{1 of the above,} and the effect in claim 1 can be easily obtained.

As in the invention of claim 5, claim 2
In the absorption refrigeration apparatus described, regeneration of the highest temperature side
Bowl G_nSolution Lc flowing out from the_nIs the hottest solution
Heat exchanger H_nThe medium temperature side with the next highest temperature after passing through the heating side of
Regenerator G_n-1Highest when configured to flow into
Regenerator G on the warm side_nConcentration flowing out from ξ_nAbsorption solution of (concentrated
Liquid) Lc_nThe heat held by the regenerator G at the highest temperature side_nTo
Concentration just before flowing in ξ_a Absorption solution (dilute solution) Lw
Will be accommodated (in other words, the regenerator on the highest temperature side)
G_nThe absorption solution (dilute solution) Lw flowing into the tank is preheated.
Therefore, the heat input from the external heat source J can be suppressed.
Wear.

As in the invention of claim 6, in the absorption refrigerating apparatus according to any one of claims 2, 3, 4 and 5, the total amount of the absorption solution Lw flowing out from the absorber A is the lowest. When configured to branch after passing through the heated side of the solution heat exchanger H _{1 on} the side, the absorbing solution Lw having the concentration ξ _a flowing out from the absorber A passes through the solution heat exchanger H ₁ on the lowest temperature side. The absorption solution (diluted solution) L, which is branched after being heated by heat recovery in the process, flows into the regenerator G _{1 on the} lowest temperature side and the regenerator G _n on the highest temperature side.
w will be preheated.

[0016] As in the invention of claim 7, in the absorption refrigerating apparatus according to any one of claims 2, 3, 4 and 5, the absorber A is provided on the solution outlet side of the absorber A.
A solution pump PL ₁ for pumping the absorbing solution Lw from the above is provided, and the absorbing solution Lw flowing out from the absorber A is provided.
However, when it is configured to branch immediately after the outlet of the solution pump PL ₁ , the absorbing solution (dilute solution) L having _a concentration of ξ _a
Immediately after the w has left the absorber A, the w is branched, and the inflow amount of the solution heat exchanger into which the branched absorption solution Lw flows is reduced, and the solution heat exchanger can be downsized.

As in the invention of claim 8, in the absorption refrigerating apparatus according to any one of claims 2, 3, 4, 5, 6 and 7, it flows into the regenerator G _n on the highest temperature side. The absorption solution Lw is the solution heat exchanger H _n on the highest temperature side.
Of the absorbing solution (dilute solution) L having _a concentration of ξ _a flowing into the regenerator G _n on the highest temperature side when it is configured to pass through the heated side of
Since w is preheated in the process of passing through the solution heat exchanger H _n on the highest temperature side, the amount of heat input from the external heat source J can be suppressed.

As in the invention of claim 9, claim
Absorption according to any one of 2, 3, 4, 5, 6 and 7.
Type refrigerating apparatus, the regenerator G on the lowest temperature side₁Flow
The absorption solution Lw to be introduced is the solution heat exchanger H on the lowest temperature side.₁
Of the regenerator G on the highest temperature side while passing through the heated side of
_nThe absorption solution Lw flowing into the is the solution heat on the lowest temperature side.
Exchanger H₁Solution heat exchanger H on the 1st stage higher temperature side₂Highest from
Solution heat exchanger H on warm side_n Solution heat exchanger up to H₂~ H_nof
When configured to pass through the heated side, the lowest temperature side
Regenerator G₁Concentration flowing into ξ_aAbsorption solution (dilute solution) Lw
Is the solution heat exchanger H on the lowest temperature side₁In the process of passing through
While being heated, the regenerator G on the highest temperature side_nConcentration flowing into
ξ_aAbsorption solution (dilute solution) Lw is the solution heat on the lowest temperature side.
Exchanger H₁Solution heat exchanger H on the 1st stage higher temperature side₂Highest from
Solution heat exchanger H on warm side_nSolution heat exchanger up to H₂~ H_nTo
It will be preheated in the process of passing through the regenerator G.₁, G_n
The thermal efficiency in is improved.

As in the invention of claim 10,
Any one of 2, 3, 4, 5, 6, 7, 8 and 9
In the absorption refrigeration equipment listed above, the highest
Regenerator G on the warm side_nAnd the regenerator G on the lowest temperature side₁Playback except
Bowl G₂~ G_n-1The absorbing solution that has flowed into the chamber is heated and becomes a refrigerant vapor.
R₂~ R_n-1To generate the respective concentration ξ₂~ Ξn_-1Concentrated
Liquid Lc₂~ Lc_n-1And each regenerator G₂~ G_n-1Outflow
And other regenerator G_n , G₁Solution Lc flowing out from
_n, Lc₁Confluence with the concentration ξ_mBefore becoming the absorption solution Lc of
When it is configured to flow into the absorber A,
Regenerator G on the hottest side_nAnd the regenerator G on the lowest temperature side₁And
Excluding regenerator G₂~ G_n-1The absorption solution flowing into the
Refrigerant vapor R₂~ R_n-1Generated and concentrated,
Degree ξ₂~ Ξn_-1Concentrated solution Lc₂~ Lc_n-1Become each play
Bowl G₂~ G_n-1Spills other regenerator G₁, G_nFlow from
Absorbed solution Lc_n, Lc₁Confluence with the concentration ξ_mAbsorption of
The solution Lc is returned to the absorber A, and the highest temperature
Side regenerator G_nAnd the regenerator G on the lowest temperature side₁Regenerator excluding and
G₂~ G_n-1In this way, efficient solution concentration can be performed.
Wear.

[0020] As in the invention of claim 11, in the absorption refrigerating apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9 and 10, the absorber A is used.
When the evaporator E is divided into a plurality of stages having different refrigerant evaporation temperatures, the one having a higher refrigerant temperature (that is, the higher pressure stage) has a lower concentration, so that the cycle can be shifted to a thinner one.

As in the invention of claim 12, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 and 11
In the absorption refrigerating apparatus according to any one of 1 to 3, when the regenerator G ₁ and the condenser C on the lowest temperature side are divided into a plurality of stages having different refrigerant condensation temperatures, one having a lower refrigerant temperature (that is, a lower pressure stage) Since the pressure can be reduced, the operating pressure can be reduced.

As in the invention of claim 13, in the absorption refrigerating apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11 and 12,
When the path of the absorbing solution is heated at least at one or more places by the residual heat after the heating of the external heat source J that heats the regenerator G _n on the highest temperature side, the residual heat after the heating of the external heat source J is used. The absorption solution will be heated,
The external heat source J can be effectively used. Case, and that the absorption solution is heated regenerator G ₁ ~G _n-1, except for the regenerator G _n of highest temperature side by steam drain Rd ₁ ~Rd _n-1 after heating, steam drain Rd ₁ ~ Rd _The heat of _n-1 can be effectively used.

As in the invention of claim 15, in the absorption refrigerating apparatus of claim 14, the solution heat exchangers H _{1 to} H _n-1 other than the solution heat exchanger H _n on the highest temperature side are heated. immediately before the side inlet branches the part of the absorbent solution, the highest temperature side of the regenerator the steam drain Rd ₁ ~ Rd after heating the regenerator G ₁ ~G _n-1, except for G _n in the branch path
_n-1 is used to heat the absorbing solution and then the solution heat exchanger H ₁
When configured to merge at the heated side outlet of to H _n-1, the regenerator G ₁ ~G except regenerator G _n of highest temperature side
Some of the absorbent solution Lw branched immediately before the heated side inlet of the _n-1 steam drain Rd ₁ after heating the ~Rd solution heat exchanger by _n-1 H ₁ to H _{n -1} is heated, after which the solution The heat exchangers H _{1 to} H _n-1 are joined at the heated side outlets, and the heat held by the steam drains Rd _{1 to} Rd _n-1 can be effectively used.

As in the invention of claim 16, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 1
In the absorption refrigeration apparatus according to any one of 2, 13, 14 and 15, the temperature difference between the inlet side temperature and the outlet side temperature of the cold water We obtained in the evaporator E is 6 ° C or more. In this case, the flow rate of the cold water We can be reduced to reduce the transport power, the refrigerant evaporation temperature can be increased, and the cycle can be shifted to the thinner side.

As in the invention of claim 17, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 1
The absorption refrigeration apparatus according to any one of 2, 13, 14, 15 and 16, wherein the condenser C and the absorber A are provided.
When the cooling water Wa that cools the cooling water is configured to flow from the condenser C to the absorber A, the pressure of the condenser C can be lowered, so that the temperature and pressure of the refrigeration cycle can be easily lowered.

As in the invention of claim 17, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 1
In the absorption refrigerating apparatus according to any one of 2, 13, 14, 15, 16 and 17, when n = 3, the temperature and pressure of the high temperature side regenerator G ₃ can be suppressed.

[0027]

DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Some preferred embodiments of the present invention will be described in detail below with reference to the accompanying drawings.

First Embodiment FIG. 1 shows a refrigerating cycle of an absorption refrigerating apparatus according to a first embodiment of the present invention.

This absorption refrigerating apparatus is an absorption refrigerating apparatus using water as a refrigerant and lithium bromide as an absorbing solution, and includes one condenser C, absorber A and evaporator E and three solution heat exchangers. Exchangers H ₃ (corresponding to H _n ), H ₂ (corresponding to H _n-1 ), H ₁ and 3
Regenerators G ₃ (corresponding to G _n ), G ₂ (corresponding to G _n-1 ), G
₁ is connected by several pipes to form a circulation cycle of the refrigerant vapor R and the absorbing solution L.

First, the basic function of each device of the absorption refrigerating apparatus shown in FIG. 1 will be explained. The evaporator E has a heat exchange section Ec through which the liquid to be cooled (cold water) We passes. The coolant (condensed water) Rc sprinkled on the heat exchange portion Ec cools the liquid to be cooled (cold water) We passing through the heat exchange portion Ec. The liquid to be cooled (cold water) We acts as a use-side cooling / heating medium and is used as a cooling / cooling heat source.
The temperature difference between the inlet side temperature and the outlet side temperature of the cold water We is 6 ° C. or more, so that the flow rate of the cold water We can be reduced to reduce the transport power and increase the refrigerant evaporation temperature. This is preferable in that the cycle can be shifted to the thinner side.

The absorber A has a function of communicating with the evaporator E and absorbing the refrigerant vapor (water vapor) Re flowing from the evaporator E into the absorbing solution Lc. Heat exchange section (cooling section) for removing generated heat absorption
It is equipped with Ac. Cooling water Wa is supplied to the heat exchange section Ac, and the cooling water Wa is further fed to a condenser C described later and is also used as condenser cooling water. The cooling water Wa may be flowed from the condenser C to the absorber A in order to reduce the pressure of the condenser C.

Three used in this absorption refrigeration system
Regenerator G₃, G₂, G₁Are the absorption solutions (diluted
(Solution) is heated and concentrated to sequentially increase the concentration ξ₃(Ξ_n), Ξ₂
(Ξ_n-1 ), Ξ₁Absorption solution (concentrated solution) Lc₃(L
c_n), Lc₂(Lc_n-1), Lc₁And
The solution pump PL from absorber A₁Sent by
Concentration ξ_aThe absorption solution (dilute solution) Lw of
Solution heat exchanger H₁Is branched after passing through the heated side of
One is the regenerator on the lowest temperature side (hereinafter referred to as the low temperature regenerator).
Say G₁Into the medium temperature side solution heat exchanger.
Exchanger H₂And high temperature solution heat exchanger H₃Highest through
Regenerator on the warm side (hereinafter referred to as high temperature regenerator) G₃Flow into
It

The high temperature regenerator G ₃ has an external heat source J (a gas combustor in this embodiment), and the absorber A
In is generated, a dilute solution Lw which has flowed through the solution heat exchanger H _1, H _2, H ₃ is heated and concentrated (i.e., while the concentrated solution Lc ₃ concentrations xi] ₃ is generated, the refrigerant temperature T ₃ Steam R ₃ (R _n
Corresponding to))). The concentrated solution Lc ₃ of concentration ξ ₃ generated in the high temperature regenerator G ₃ flows into the medium temperature regenerator G ₂ of the next stage through the heating side of the solution heat exchanger H ₃ .

[0034] In the intermediate temperature regenerator G _2, the high temperature regenerator G ₃ refrigerant vapor R ₃ generated by the introduction, the solution heat exchanger from said high temperature generator G ₃ by the heat held by the refrigerant vapor R ₃ absorption solution having a concentration xi] ₃ flowing through the vessel H ₃ (strong solution) is heated and concentrated (i.e., while the concentrated solution Lc ₂ concentration xi] ₂ is produced, the refrigerant vapor R ₂ temperature T ₂ (R _n Corresponding to _-1 ))). The concentrated solution Lc ₂ of concentration ξ ₂ generated in the medium temperature regenerator G ₂ returns to the absorber A through the heating sides of the solution heat exchangers H ₂ and H ₁ .

The low temperature regenerator G₁At the medium temperature
Regenerator G₂Refrigerant vapor R generated in₂ Is introduced, the refrigerant
Steam R₂Solution heat from the absorber A due to the heat held by
Exchanger H₁Concentration that branches and flows in after passing through_aSucking
The concentrated solution (dilute solution) Lw is heated and concentrated (that is, the concentration ξ
₁Concentrated solution Lc₁Is generated while the temperature T₁Refrigerant vapor of
R₁To generate). The low temperature regenerator G₁Concentration generated by
₁Concentrated solution L₁Is the medium temperature regenerator G₂Concentration discharged from
ξ₂Concentrated solution Lc₂Confluence with the concentration ξ_mOf concentrated solution Lc
Solution heat exchanger H₁Return to absorber A through the heating side of
It

[0036] In the above condenser C, the low temperature generator refrigerant vapor R ₁ generated in G ₁ is introduced, the refrigerant vapor R
₁ is cooled and condensed by the cooling water Wa that passes through the heat exchange section Cc (in the embodiment of FIG. 1, the cooling water after passing through the absorber A);
Liquid refrigerant (condensed water) Rc is generated. The refrigerant vapor R ₃ introduced into the medium temperature regenerator G ₂ and the refrigerant vapor R ₂ introduced into the low temperature regenerator G ₁ are both vapor drains Rd ₂ and Rd _1.
After the steam drains Rd ₂ and Rd ₁ merge,
It is sent to the condenser C. The liquid refrigerant Rc generated in the condenser C is supplied to the evaporator E.

Solution heat exchanger H₁, H₂, H₃Each re
Organ G₁, G₂, G₃Concentrated solution Lc produced by₁, Lc₂，
Lc₃Diluted solution Lw that flows out of heat from the absorber A
For recovering heat to the solution heat exchanger H₃Addition of
High temperature regenerator G on the heat side₃Concentrated solution Lc flowing out from₃Led by
Put in, solution heat exchanger H₂On the heating side of the₂
Concentrated solution Lc flowing out from₂Is introduced into the solution heat exchanger H₁
On the heating side of the₂Solution flow out after flowing out from
Exchanger H₂Solution Lc that passed through the heating side of₂And low temperature regenerator G
₁Concentrated solution Lc flowing out from₁To be introduced by joining
Has become.

Further, in this embodiment, the external heat source
High temperature regenerator G due to residual heat of J₃ Concentration supplied to_a
The exhaust heat heat exchanger K for preheating the absorbing solution (dilute solution) Lw of
It is attached. In this way, heating of the external heat source J
The absorption solution (dilute solution) Lw is preheated by the residual heat afterwards.
As a result, the external heat source J can be effectively used.
Further, in the present embodiment, the high temperature regenerator G₃Excluding
Regenerator G₁, G₂Each steam drain Rd after heating₁, Rd₂
And the solution heat exchanger H₁, H₂Immediately before the heated side entrance of
Heat exchange with a branched solution obtained by branching a part of the absorption solution Lw
Drain heat exchanger D₁, D₂Is attached. Na
The branch solution is the drain heat exchanger D.₁, D₂Suck after passing through
Combined with the collecting solution Lw. This way, high temperature regeneration
Bowl G_nRegenerator G except₁, G₂Drain R after heating
d₁, Rd₂Solution heat exchanger by₁, H₂On the heated side
Immediately before the mouth, part of the branched absorption solution Lw was heated.
Solution heat exchanger H₁, H₂At the heated side outlet
Will be joined together and steam drain Rd₁, Rd₂Protection
It is possible to effectively utilize the heat that the user has.

The state change of the absorbing solution in the absorption refrigerating apparatus having the above structure is as shown in the Duhring diagram shown in FIG.

[0040] By the structure described above, the concentration range in the low temperature regenerator G ₁ of the most low-temperature side (ξ ₁ -ξ _a) and highest temperature side of the density width in the high temperature generator ξ ₃ (ξ ₃ -ξ _a )
Becomes smaller than the concentration width (ξ _m −ξ _a ) between the inlet and the outlet of the absorber A. Therefore, it is possible to reduce the temperature and pressure in the refrigeration cycle, and it is possible to reduce the transport power and the strength of each element that constitutes the refrigeration cycle, thereby reducing the cost and the risk of corrosion.

Moreover, in the present embodiment, the absorbing solution (dilute solution) Lw having the concentration ξ _a flowing out from the absorber A is branched, and one of them is introduced into the lowest temperature side low temperature regenerator G ₁ ,
The other is the high temperature regenerator G ₃ where the total amount of branching is the highest temperature side.
Is designed to flow into the high temperature regenerator G ₃
Since the flow rate of the absorbing solution (dilute solution) Lw having the concentration ξ _a flowing into the can be reduced, the sensible heat content of the absorbing solution Lw that is heated and boiled decreases. Therefore, the heat input to the regenerator is reduced, and the COP is improved.

Further, in the present embodiment, the absorbing solution (concentrated solution) Lc _{3 having} the concentration ξ ₃ flowing out from the high temperature regenerator G _{3 is} discharged.
But it is configured so as to pass through the heating side of the solution heat exchanger H ₃ immediately before flowing into the high-temperature regenerator G ₃ flowing into the intermediate temperature regenerator G _2, flows out from the high temperature regenerator G ₃ The heat possessed by the absorbing solution (concentrated solution) Lc _{3 having} the concentration ξ ₃ is recovered in the absorbing solution (dilute solution) Lw having the concentration ξ _a immediately before flowing into the high temperature regenerator G ₃ (in other words, , The absorption solution (dilute solution) Lw flowing into the high temperature regenerator G ₃ is preheated), and the heat input amount from the external heat source J can be suppressed.

In the present embodiment, the absorber A
Outflow from ξ_aThe total amount of the absorption solution Lw of
Exchanger H₁Is configured to branch after passing through the heated side of
Therefore, the concentration ξ flowing out from absorber A_aAbsorption solution of
Lw is the solution heat exchanger H₁Heat recovery in the process of passing through
It will be branched after being heated, and the low temperature regenerator G₁
And high temperature regenerator G₃Absorption solution (dilute solution) L
w will be preheated.

Further, in the present embodiment, low temperature regeneration
Bowl G₁Concentration flowing into ξ_aThe absorption solution (dilute solution) Lw of
Solution heat exchanger H₁High temperature regeneration while passing through the heated side of
Bowl G₃ Concentration flowing into ξ_aThe absorption solution (dilute solution) Lw of
Solution heat exchanger H₁, H₂, H₃To pass through the heated side of
Since it is configured in the low temperature regenerator G₁Concentration flowing into
ξ_aThe absorbing solution (dilute solution) Lw of is the solution heat exchanger H₁Through
High temperature regenerator G while being preheated in the process of passing₃Flow into
Concentration ξ_aAbsorption solution (dilute solution) Lw is a solution heat exchanger
H₁, H₂, H₃It will be preheated in the process of passing through
Regenerator G₁, G₃The thermal efficiency in is improved.

Further, in this embodiment, the highest temperature
Side high temperature regenerator G₃And the lowest temperature side low temperature regenerator G₁Excluding and
Medium temperature regenerator G₂The absorption solution flowing into
Steam R₂Generate the concentration ξ₂Becomes a concentrated solution of regenerator G₂
Spills other regenerator G₁ , G₃Outflow from ξ
₁, Ξ₃Absorption solution (concentrated solution) Lc₁, Lc₃Confluence with
Degree ξ_mSo that it becomes the absorbing solution Lc and flows into absorber A.
Since it is configured in the high temperature regenerator G₃And low temperature regenerator G₁
Regenerator G excluding and₂To efficiently concentrate the solution in
You can

Second Embodiment FIG. 3 shows a refrigerating cycle of an absorption refrigerating apparatus according to a second embodiment of the present invention.

In this case, the concentration ξ flowing out from the absorber A_a
Absorption solution (dilute solution) Lw of the solution heat exchanger H on the low temperature side
₁After passing through the heated side, it is branched into three, one of which
Is a low temperature regenerator G₁Flow into the
Liquid heat exchanger H₃And passing through the heated side of the exhaust heat exchanger K
And high temperature regenerator G₃The last one is on the medium temperature side
Solution heat exchanger H₂Passing through the heated side of the medium temperature regenerator G₂To
It is flowing in. Also, the high temperature regenerator G₃Concentration flowing out of
ξ₃Concentrated solution Lc₃Is the solution heat exchanger H on the high temperature side.₃Heating
After passing the side, medium temperature regenerator G₂Medium temperature after spilled from
Solution heat exchanger H on the side₂ Concentration passed through₂Concentrated solution Lc₂
And low temperature regenerator G₁Outflow from ξ₁Concentrated solution Lc
₁Confluence with the concentration ξ_mAbsorption solution (concentrated solution) Lc of
After that, the solution heat exchanger H on the low temperature side₁Passing through the heating side of the
It is supposed to return to collector A. In addition, in the present embodiment
The flow of cooling water that cools the absorber A and the condenser C
The direction is opposite to that in the first embodiment (that is,
The condenser C is changed to the absorber A). Do this
And the pressure of the condenser C can be reduced,
As in the embodiment, even if the absorber A → condenser C
Good.

The state change of the absorbing solution in the absorption refrigerating apparatus having the above-mentioned structure is as shown in the Duhring diagram shown in FIG. Also in this case, the concentration width (ξ ₁ −ξ _a ) in the lowest temperature side low temperature regenerator G ₁ and the highest temperature side high temperature regenerator ξ ₃
The concentration width (ξ ₃ −ξ _a ) at is smaller than the concentration width (ξ _m −ξ _a ) between the inlet and the outlet of the absorber A.

The rest of the configuration, functions, and effects are the same as in the first embodiment, so a description thereof will be omitted.

Third Embodiment FIG. 5 shows a refrigeration cycle of an absorption type refrigeration system according to a third embodiment of the present invention.

In this case, the concentration ξ flowing out of the absorber A_a
Absorption solution (dilute solution) Lw of the solution heat exchanger H on the low temperature side
₁Branch before flowing into the other, one is the solution heat exchange on the low temperature side
Bowl H₁ Low temperature regenerator G through the heated side of₁Flowing into the other
Is the solution heat exchanger H on the medium temperature side.₂After passing through the heated side of
One is the medium temperature regenerator G.₂The other,
Solution heat exchanger H on the high temperature side₃And addition of the exhaust heat heat exchanger K
High temperature regenerator G passing through the heat side₃Is flowing into. Tsuma
, Part of the branched absorption solution (dilute solution) Lw is regenerated at high temperature
Bowl G₃It is supposed to flow into. Also high
Temperature regenerator G₃Outflow from ξ₃Concentrated solution Lc₃Is high
Solution heat exchanger H on warm side₃After passing the heating side of the
Regenerator G₂Outflow from ξ₂Concentrated solution Lc₂Joins
Solution heat exchanger H on the medium temperature side₂Passing through the heating side of the
Rear low temperature regenerator G₁Solution heat exchange on the low temperature side after flowing out from
Bowl H₁Concentration passing through the heating side of₁Concentrated solution Lc₁Joins
Then the concentration ξ_mReturn to absorber A as concentrated solution Lc of
Has become. In this way, the concentration ξ_aAbsorption solution of
(Dilute solution) Lw is branched immediately after leaving the absorber A
And the solution heat exchanger H on the low temperature side₁The flow rate of the
Can be modeled. In addition, in the present embodiment,
The flow direction of the cooling water for cooling the collector A and the condenser C is the first
In the opposite direction (ie, condenser C → suction
It is a collector A). By doing this, the condenser C
The pressure can be reduced, but in the first embodiment
As described above, the absorber A may be changed to the condenser C.

The state change of the absorbing solution in the absorption refrigerating apparatus having the above structure is as shown in the Duhring diagram shown in FIG. Also in this case, the concentration width (ξ ₁ −ξ _a ) in the lowest temperature side low temperature regenerator G ₁ and the highest temperature side high temperature regenerator ξ ₃
The concentration width (ξ ₃ −ξ _a ) at is smaller than the concentration width (ξ _m −ξ _a ) between the inlet and the outlet of the absorber A.

The rest of the configuration, functions and effects are the same as those of the first embodiment, so the description thereof will be omitted.

Fourth Embodiment FIG. 7 shows a refrigeration cycle of an absorption refrigeration system according to a fourth embodiment of the present invention.

In this case, the concentration ξ flowing out from the absorber A_a
Absorption solution (dilute solution) Lw of the solution heat exchanger H on the low temperature side
₁Is branched after passing through the heated side of the
Temperature regenerator G₂Flow into the other, the other is the solution heat exchange on the high temperature side.
Exchanger H₃And passing through the heated side of the exhaust heat exchanger K
Temperature regenerator G₃Is flowing into. Also, the low temperature regenerator G₁From
Outflowing concentration ξ₁Concentrated solution Lc₁Is the solution pump PL₂of
Solution heat exchanger H on the medium temperature side due to the pressure-feeding force₂The heated side of
Pass the medium temperature regenerator G₂Is supposed to flow into.
Also, the high temperature regenerator G₃Concentration flowing out from ξ₃Concentrated solution Lc
₃Is the solution heat exchanger H on the high temperature side.₃After passing through the heating side of
Medium temperature regenerator G₂Solution heat exchanger on the medium temperature side after flowing out from
H₂Concentration passed through₂Concentrated solution Lc₂Confluence with the concentration ξ_m
It becomes a concentrated solution Lc of and returns to the absorber A.
It By doing this, the low temperature regenerator G₁ More outflow
Degree ξ₁Absorption solution (concentrated solution) Lc₁However, the medium temperature regenerator G₂To
High temperature regenerator G₃Refrigerant vapor R generated in₃Heated by the heat of
Boiled and further concentrated to give a concentration ξ₂Absorption solution of (concentrated
Liquid) Lc₂Will be In addition, in the present embodiment
The flow of cooling water that cools absorber A and condenser C
The direction is opposite to that in the first embodiment (that is,
Compressor C → absorber A). This way,
Although the pressure of the condenser C can be reduced,
As in the form, absorber A → condenser C
Yes.

The state change of the absorbing solution in the absorption type refrigerating apparatus having the above-mentioned structure is as shown in a Duhring diagram shown in FIG. Also in this case, the concentration width (ξ ₁ −ξ _a ) in the lowest temperature side low temperature regenerator G ₁ and the highest temperature side high temperature regenerator ξ ₃
The concentration width (ξ ₃ −ξ _a ) at is smaller than the concentration width (ξ _m −ξ _a ) between the inlet and the outlet of the absorber A.

The rest of the configuration, functions and effects are the same as in the first embodiment, so a description thereof will be omitted.

Fifth Embodiment FIG. 9 shows a refrigeration cycle of an absorption refrigeration system according to a fifth embodiment of the present invention.

In this case, the absorber A and the evaporator E are cooled
Two stages with different medium evaporation temperatures (that is, low-pressure absorber A₁and
High pressure absorber A₂And low pressure evaporator E₁And high-pressure evaporator E₂)
Is divided into In addition, the lowest temperature low temperature regenerator G₁
And the condenser C has two stages (ie,
High-pressure regeneration section G₁₁And low pressure regeneration unit G₁₂And high pressure condenser C₁
And low pressure condenser C₂) Is divided into.

[0060] In the evaporator E, the condensed water Rc from the condenser C is supplied to the low pressure evaporator section E _1, the low pressure evaporator section E ₁
And the refrigerant vapor Re generated in the high-pressure evaporator E ₂ are respectively the low-pressure absorber A ₁ and the high-pressure absorber A _{2 in the} absorber A.
Sent to.

In the absorber A, the low pressure absorber A ₁
The concentrated solution Lc is returned to the high pressure absorption part A ₂ and diluted solution Lw
Will be leaked.

The low temperature regenerator G₁In the absorber A
The dilute solution Lw from the high pressure regenerator G₁₁ Flowing into the dilute solution
Concentrated solution Lc obtained by concentrating Lw by heating and boiling
₁Is the low-pressure regeneration unit G₁₂High pressure due to boiling
Playback part G₁₁And low pressure regeneration unit G₁₂Occur in
Refrigerant vapor R₁Are high-pressure condensations in condenser C, respectively.
Reduced part C₁And low pressure condenser C₂To be sent to
It

Also, the refrigerant vapor R from the medium temperature regenerator G _2
2 flows into the low-pressure regenerator G ₁₂ in the low-temperature regenerator G ₁ and then flows out from the high-pressure regenerator G ₁₁ and the drain heat exchanger D
It is supposed to flow into the low-pressure condenser section C ₂ of the condenser C via ₁

By doing so, as shown by the dotted line → solid line in the During diagram of FIG. 10, in the absorber A and the evaporator E, the concentration decreases in the higher refrigerant temperature (that is, in the high pressure stage). Therefore, the cycle can be shifted to the thinner side, and in the low temperature regenerator G ₁ and the condenser C, the pressure can be lowered in the side where the refrigerant temperature is low (that is, the low pressure stage), and the operating pressure can be reduced.

In the present embodiment, both the absorber A and the evaporator E and the low temperature regenerator G ₁ and the condenser C are divided, but the absorber A, the evaporator E or the low temperature regenerator G is divided.
Either _{one of} the condenser ₁ and the condenser C may be divided.

The rest of the configuration, functions and effects are the same as those in the first embodiment, so the explanation is omitted.

Sixth Embodiment FIG. 11 shows a refrigerating cycle of an absorption refrigerating apparatus according to a sixth embodiment of the present invention.

In this case, the refrigeration cycle is the same as that in the second embodiment described above, and the absorbing solution (dilute solution) Lw having the concentration ξ _a flowing out from the absorber A is the solution heat exchange on the low temperature side. After passing through the heated side of the vessel H ₁ , it is branched into three, _{one of} which flows into the low temperature regenerator G ₁ and the other of which enters the high temperature side solution heat exchanger H ₃ and exhaust heat exchange. flows into the high-temperature regenerator G ₃ through the heated side of the vessel K, last one, the solution heat exchanger of H ₂ medium temperature side through the heated side flows into the intermediate temperature regenerator G ₂ ing. Further, the concentrated solution Lc ₃ of concentration ξ ₃ flowing out from the high temperature regenerator G ₃ passes through the heating side of the solution heat exchanger H ₃ on the high temperature side, and then flows out from the intermediate temperature regenerator G ₂ and then the medium temperature side solution. concentrations xi] ₂ which has passed through the heat exchanger H ₂ concentrated solution Lc ₂ and the low-temperature regenerator concentration xi] ₁ flowing out of the G ₁
Of the concentrated solution Lc ₁ into a concentrated solution Lc having a concentration of ξ _m ,
After that, it passes through the heating side of the solution heat exchanger H ₁ on the low temperature side and returns to the absorber A.

Moreover, the absorber A and the evaporator E are divided into two stages having different refrigerant evaporation temperatures (that is, the low pressure absorption section A ₁ and the high pressure absorption section A ₂ and the low pressure evaporation section E ₁ and the high pressure evaporation section E ₂ ). Has been done. Further, the low temperature regenerator G ₁ and the condenser C on the lowest temperature side have two stages having different refrigerant condensing temperatures (that is, the high pressure regenerating section G ₁₁ and the low pressure regenerating section G ₁₂ , the high pressure condensing section C ₁ and the low pressure condensing section C _2). ) Is divided into.

[0070] In the evaporator E, the condensed water Rc from the condenser C is supplied to the low pressure evaporator section E _1, the low pressure evaporator section E ₁
And the refrigerant vapor Re generated in the high-pressure evaporator E ₂ are respectively the low-pressure absorber A ₁ and the high-pressure absorber A _{2 in the} absorber A.
Sent to.

In the absorber A, the low pressure absorber A ₁
The concentrated solution Lc is returned to the high pressure absorption part A ₂ and diluted solution Lw
Will be leaked.

The low temperature regenerator G₁In the absorber A
The dilute solution Lw from the high-pressure regeneration section G₁₁ Flowing into the dilute solution
Concentrated solution Lc obtained by concentrating Lw by heating and boiling
₁Is the low-pressure regeneration unit G₁₂High pressure due to boiling
Playback part G₁₁And low pressure regeneration unit G₁₂Occur in
Refrigerant vapor R₁Are high-pressure condensations in condenser C, respectively.
Reduced part C₁And low pressure condenser C₂To be sent to
It

Also, the refrigerant vapor R from the medium temperature regenerator G _2
2 branches before the low-temperature regenerator G ₁ and flows into the low-pressure regeneration section G ₁₁ and the high-pressure regeneration section G ₁₂ in parallel, then flows out from the high-pressure regeneration section G ₁₁ and the low-pressure regeneration section G _12, and then merges. , Through the drain heat exchanger D ₁ into the low-pressure condenser C ₂ of the condenser C.

Further, the way of flowing the cooling water Wa is different from that in the fifth embodiment, that is, the low pressure absorbing section A ₁ and the high pressure absorbing section A _{2 in the} absorber A, and the low pressure condensing section C ₁ in the condenser C and It is adapted to be supplied in parallel to the high-pressure condenser C ₂ .

By doing so, as shown by the dotted line and the solid line in the During diagram of FIG. 12, in the absorber A and the evaporator E, the concentration decreases in the higher refrigerant temperature (that is, in the high pressure stage). Therefore, the cycle can be shifted to the thinner side, and in the low temperature regenerator G ₁ and the condenser C, the pressure can be lowered in the side where the refrigerant temperature is low (that is, the low pressure stage), and the operating pressure can be reduced.

In this embodiment, both the absorber A and the evaporator E and the low temperature regenerator G ₁ and the condenser C are divided, but the absorber A, the evaporator E or the low temperature regenerator G is divided.
Either _{one of} the condenser ₁ and the condenser C may be divided.

Further, in the present embodiment, _both the parallel supply system of the refrigerant vapor R ₂ to the low temperature regenerator G ₁ and the parallel supply system of the cooling water Wa to the absorber A and the condenser C are implemented. However, you may make it implement in any one or only two.

The other structure, functions and effects are the same as those in the first embodiment, and the explanation thereof is omitted.

Seventh Embodiment FIG. 13 shows a refrigeration cycle of an absorption refrigeration system according to a seventh embodiment of the present invention.

In this case, the refrigeration cycle is the same as in the above-described fourth embodiment, and the absorbing solution (dilute solution) Lw having the concentration ξ _a flowing out from the absorber A is the solution heat exchange on the low temperature side. Branched after passing through the heated side of the vessel H ₁ ,
One flows into the low temperature regenerator G ₁ , and the other flows into the high temperature regenerator G ₃ after passing through the solution heat exchanger H ₃ on the high temperature side and the heated side of the exhaust heat heat exchanger K. is doing. Further, the concentrated solution Lc ₁ having the concentration ξ ₁ flowing out from the low temperature regenerator G ₁ passes through the heated side of the medium temperature side solution heat exchanger H ₂ by the pumping force of the solution pump PL ₂ and the medium temperature regenerator G ₂ Is supposed to flow into. Further, the concentrated solution Lc ₃ of concentration ξ ₃ flowing out from the high temperature regenerator G ₃ passes through the heating side of the solution heat exchanger H ₃ on the high temperature side, and then flows out from the intermediate temperature regenerator G ₂ and then the medium temperature side solution. concentrations xi] ₂ which has passed through the heat exchanger H ₂ concentrated solution Lc ₂
And the concentrated solution Lc having a concentration of ξ _m is returned to the absorber A.

Moreover, the absorber A and the evaporator E are divided into two stages having different refrigerant evaporation temperatures (that is, the low pressure absorption section A ₁ and the high pressure absorption section A ₂ and the low pressure evaporation section E ₁ and the high pressure evaporation section E ₂ ). Has been done. Further, the low temperature regenerator G ₁ and the condenser C on the lowest temperature side have two stages having different refrigerant condensing temperatures (that is, the high pressure regenerating section G ₁₁ and the low pressure regenerating section G ₁₂ , the high pressure condensing section C ₁ and the low pressure condensing section C _2). ) Is divided into.

[0082] In the evaporator E, the condensed water Rc from the condenser C is supplied to the low pressure evaporator section E _1, the low pressure evaporator section E ₁
And the refrigerant vapor Re generated in the high-pressure evaporator E ₂ are respectively the low-pressure absorber A ₁ and the high-pressure absorber A _{2 in the} absorber A.
Sent to.

In the absorber A, the low pressure absorber A ₁
The concentrated solution Lc is returned to the high pressure absorption part A ₂ and diluted solution Lw
Will be leaked.

The low temperature regenerator G₁In the absorber A
The dilute solution Lw from the high-pressure regeneration section G₁₁ Flowing into the dilute solution
Concentrated solution Lc obtained by concentrating Lw by heating and boiling
₁Is the low-pressure regeneration unit G₁₂High pressure due to boiling
Playback part G₁₁And low pressure regeneration unit G₁₂Occur in
Refrigerant vapor R₁Are high-pressure condensations in condenser C, respectively.
Reduced part C₁And low pressure condenser C₂To be sent to
It

Also, the refrigerant vapor R from the medium temperature regenerator G _2
2 branches before the low temperature regenerator G ₁ and flows in parallel to the high temperature regeneration unit G ₁₁ and the low pressure regeneration unit G ₁₂ , and then flows out from the high pressure regeneration unit G ₁₁ and the low pressure regeneration unit G ₁₂ and merges. , Through the drain heat exchanger D ₁ into the low-pressure condenser C ₂ of the condenser C.

Further, the way of flowing the cooling water Wa is different from that of the fifth embodiment, that is, the low-pressure absorbing section A ₁ and the high-pressure absorbing section A _{2 in the} absorber A and the high-pressure condensing section C _{1 in the} condenser C.
And is supplied in parallel to the low pressure condenser C ₂ .

By doing so, as shown by the dotted line → solid line in the During diagram of FIG. 14, in the absorber A and the evaporator E, the concentration decreases in the higher refrigerant temperature (that is, in the high pressure stage). Therefore, the cycle can be shifted to the thinner side, and in the low temperature regenerator G ₁ and the condenser C, the pressure can be lowered in the side where the refrigerant temperature is low (that is, the low pressure stage), and the operating pressure can be reduced.

In the present embodiment, both the absorber A and the evaporator E and the low temperature regenerator G ₁ and the condenser C are divided, but the absorber A, the evaporator E or the low temperature regenerator G is divided.
Either _{one of} the condenser ₁ and the condenser C may be divided.

Further, in the present embodiment, _both the parallel supply system of the refrigerant vapor R ₂ to the low temperature regenerator G ₁ and the parallel supply system of the cooling water Wa to the absorber A and the condenser C are implemented. However, you may make it implement in any one or only two.

The other construction, function and effect are the same as those in the first embodiment, and the explanation thereof will be omitted.

Eighth Embodiment FIG. 15 shows a refrigeration cycle of an absorption refrigeration system according to an eighth embodiment of the present invention.

In this case, the concentration ξ flowing out from the absorber A_a
Absorption solution (dilute solution) Lw of the solution heat exchanger H on the low temperature side
₁Branch before flowing into the other, one is the solution heat exchange on the low temperature side
Bowl H₁ Low temperature regenerator G through the heated side of₁Flowing into the other
Is a solution heat exchanger H whose total amount is the medium temperature side.₂, High temperature side solution heat
Exchanger H₃And passing through the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, the high temperature regenerator G₃Or
Outflow concentration ξ₃Concentrated solution Lc₃Is the solution heat exchange on the high temperature side
Exchanger H₃After passing through the heating side of the₂ Flowing into
It is supposed to do. In addition, the medium temperature regenerator G₂Flow from
Concentrated concentration ξ₂Concentrated solution Lc₂Is the solution heat exchanger on the medium temperature side
H₂After passing through the heating side of the low temperature regenerator G₁Leaked from
Solution heat exchanger H on the low temperature side₁Passed through the heating side of
Degree ξ₁Concentrated solution Lc₁Confluence with the concentration ξ_mOf concentrated solution Lc
It is supposed to return to absorber A.

Absorption melting in the absorption type refrigerating apparatus having the above structure.
The state change of the liquid is as shown in the Duhring diagram shown in FIG.
Becomes Also in this case, the lowest temperature low temperature regenerator G₁To
Concentration range (ξ₁−ξ_a) And the highest temperature regenerator ξ
₃Concentration range at (ξ₃−ξ_a ) Is the inlet and outlet of absorber A
Concentration range with (ξ_m−ξ_a) Is smaller.

The other structure, function and effect are the same as those in the first embodiment, and the explanation thereof is omitted.

Ninth Embodiment FIG. 17 shows a refrigerating cycle of an absorption refrigerating apparatus according to a ninth embodiment of the present invention.

In this case, the concentration ξ _a flowing out of the absorber A
Absorption solution (dilute solution) Lw of the solution heat exchanger H on the low temperature side
After passing through the heated side of ₁ , one of them is branched into the low temperature regenerator G ₁ and the other is further branched after passing through the medium temperature side solution heat exchanger H _2. One is
It flows into the medium temperature regenerator G ₂ , and the other flows into the high temperature regenerator G ₃ after passing through the solution heat exchanger H ₃ on the high temperature side and the heated side of the exhaust heat heat exchanger K. Further, the concentrated solution Lc ₃ concentrations xi] ₃ flowing out from the high temperature regenerator G ₃ are, after passing through the heating side of the solution heat exchanger H ₃ on the high temperature side, the concentration xi] ₂ flowing out of the intermediate temperature regenerator G ₂ conc After confluence with the solution Lc ₂ and then passing through the solution heat exchanger H ₂ on the intermediate temperature side, it merges with the concentrated solution Lc ₁ of the concentration ξ ₁ flowing out from the low temperature regenerator G ₁ to form a concentrated solution Lc of the concentration ξ _m. Then, it passes through the heating side of the solution heat exchanger H ₁ on the low temperature side and returns to the absorber A.

Absorption melting in the absorption refrigerating apparatus having the above structure
The state change of the liquid is as shown in the Duhring diagram shown in FIG.
Becomes Also in this case, the lowest temperature low temperature regenerator G₁To
Concentration range (ξ₁−ξ_a) And the highest temperature regenerator ξ
₃Concentration range at (ξ₃−ξ_a ) Is the inlet and outlet of absorber A
Concentration range with (ξ_m−ξ_a) Is smaller.

The other structure, function and effect are the same as those in the first embodiment, and therefore the explanation thereof is omitted.

Tenth Embodiment FIG. 19 shows a refrigerating cycle of an absorption refrigerating apparatus according to a tenth embodiment of the present invention.

In this case, the concentration ξ flowing out from the absorber A_a
Absorption solution (dilute solution) Lw of the solution heat exchanger H on the low temperature side
₁Branch before flowing into the other, one is the solution heat exchange on the low temperature side
Bowl H₁ Low temperature regenerator G through the heated side of₁Flowing into the other
Is further branched, and one is the solution heat exchanger H on the medium temperature side.₂
Medium temperature regenerator G through the heated side of₂Flowing into and another
Is the solution heat exchanger H on the high temperature side.₃And the exhaust heat exchanger K
High temperature regenerator G passing through the heated side₃Is flowing into. One
Part of the branched absorption solution (dilute solution) Lw is reheated at high temperature.
Organ G₃It is supposed to flow into. Also,
High temperature regenerator G₃Outflow from ξ₃Concentrated solution Lc₃When,
Medium temperature regenerator G₂Outflow from ξ₂Concentrated solution Lc₂When
Are the solution heat exchangers H on the high temperature side and the medium temperature side, respectively.₃，
H₂After passing through the heating side of the low temperature regenerator G₁Leaked from
Solution heat exchanger H on the low temperature side₁Passed through the heating side of
Degree ξ₁Concentrated solution Lc₁Confluence with the concentration ξ_mOf concentrated solution Lc
It is supposed to return to absorber A.

Absorption dissolution in the absorption type refrigeration system configured as described above.
The state change of the liquid is as shown in the Duhring diagram shown in FIG.
Becomes Also in this case, the lowest temperature low temperature regenerator G₁To
Concentration range (ξ₁−ξ_a) And the highest temperature regenerator ξ
₃Concentration range at (ξ₃−ξ_a ) Is the inlet and outlet of absorber A
Concentration range with (ξ_m−ξ_a) Is smaller.

The other structure, function and effect are the same as those in the first embodiment, and the explanation thereof is omitted.

Eleventh Embodiment FIG. 21 shows a refrigeration cycle of an absorption refrigeration system according to an eleventh embodiment of the present invention.

In this case, the same as in the fourth embodiment.
The refrigeration cycle is as follows, and it flowed out from the absorber A.
Concentration ξ_aAbsorption solution (dilute solution) Lw of the solution heat on the low temperature side
Exchanger H₁After passing through the heated side of the
One is the low temperature regenerator G₁The other side of the high temperature side
Solution heat exchanger H₃And the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, low temperature regeneration
Bowl G₁Outflow from ξ₁Concentrated solution Lc₁The solution pong
LP₂Solution heat exchanger H on the medium temperature side due to the pumping force of₂ Cover
Medium temperature regenerator G passing through the heating side₂Will flow into
However, part of it is in the absorption solution return circuit to absorber A.
It is supposed to be branched. Also, the high temperature regenerator G₃Or
Concentration flowing out from_aConcentrated solution Lc₃Is the solution heat exchange on the high temperature side
Exchanger H₃After passing through the heating side of the₂Spilled from
Solution heat exchanger H on the medium temperature side₂Concentration passed through₂of
Concentrated solution Lc₂Joined with the low temperature regenerator G₁Spilled from
And the solution pump LP₂Concentration branched off at the exit side of₁
Concentrated solution Lc₁Confluence with the concentration ξ_m Of concentrated solution Lc
It is supposed to return to absorber A. This way,
Low temperature regenerator G₁Outflowing concentration ξ₁Absorption solution of (concentrated
Liquid) Lc₁However, the medium temperature regenerator G₂ At high temperature regenerator G₃so
Generated refrigerant vapor R₃It is heated to boiling by the heat of and further concentrated
Concentrated ξ₂Absorption solution (concentrated solution) Lc₂And
Become.

Absorption melting in the absorption type refrigerating apparatus having the above structure.
The state change of the liquid is as shown in the Duhring diagram shown in FIG.
Becomes Also in this case, the lowest temperature low temperature regenerator G₁To
Concentration range (ξ₁−ξ_a) And the highest temperature regenerator ξ
₃Concentration range at (ξ₃−ξ_a ) Is the inlet and outlet of absorber A
Concentration range with (ξ_m−ξ_a) Is smaller.

The other structure, function and effect are the same as those in the first embodiment, and therefore the explanation thereof is omitted.

Twelfth Embodiment FIG. 23 shows a refrigerating cycle of an absorption refrigerating apparatus according to a twelfth embodiment of the present invention.

In this case, the concentration ξ flowing out from the absorber A_a
Absorption solution (dilute solution) Lw of the solution heat exchanger H on the low temperature side
₁Branch before flowing into the other, one is the solution heat exchange on the low temperature side
Bowl H₁ Low temperature regenerator G through the heated side of₁Flowing into the other
Is the solution heat exchanger H on the high temperature side₃And waste heat heat exchange
High-temperature regenerator G passing through the heated side of vessel K₃Is flowing into
It Also, the low temperature regenerator G₁Outflow from ξ₁Concentrated solution of
Lc₁Is the solution pump PL₂ Of the medium temperature side by the pumping force of
Liquid heat exchanger H₂Passing through the heated side of the medium temperature regenerator G₂ Flow
It is supposed to enter. Also, the high temperature regenerator G₃Flow from
Concentrated concentration ξ₃Concentrated solution Lc₃Is a medium temperature regenerator G₂Flow from
After discharging, the solution heat exchanger H on the medium temperature side and the low temperature side₂, H₁of
Concentration passed through heating side ξ₂Concentrated solution Lc₂Confluence with concentration
ξ_mOf concentrated solution Lc and returned to absorber A
There is. By doing this, the low temperature regenerator G₁More outflow
Concentration ξ₁Absorption solution (concentrated solution) Lc₁However, the medium temperature regenerator G₂
At high temperature regenerator G₃Refrigerant vapor R generated in₃Added by the heat of
It is heated to boiling and further concentrated to give a concentration ξ₂Absorption solution of
Solution) Lc₂Will be .

Absorption melting in the absorption type refrigerating apparatus having the above structure
The state change of the liquid is as shown in the Duhring diagram shown in FIG.
Becomes Also in this case, the lowest temperature low temperature regenerator G₁To
Concentration range (ξ₁−ξ_a) And the highest temperature regenerator ξ
₃Concentration range at (ξ₃−ξ_a ) Is the inlet and outlet of absorber A
Concentration range with (ξ_m−ξ_a) Is smaller.

The other structure, function and effect are the same as those in the first embodiment, and the description thereof will be omitted.

Thirteenth Embodiment FIG. 25 shows a refrigerating cycle of an absorption refrigerating apparatus according to a thirteenth embodiment of the present invention.

In this case, the same as in the fourth embodiment.
The refrigeration cycle is as follows, and it flowed out from the absorber A.
Concentration ξ_aAbsorption solution (dilute solution) Lw of the solution heat on the low temperature side
Exchanger H₁After passing through the heated side of the
One is the low temperature regenerator G₁The other side of the high temperature side
Solution heat exchanger H₃And the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, low temperature regeneration
Bowl G₁Outflow from ξ₁Concentrated solution Lc₁The solution pong
PL₂Solution heat exchanger H on the medium temperature side due to the pumping force of₂ Cover
Medium temperature regenerator G passing through the heating side₂Will flow into
ing. Also, the high temperature regenerator G₃Concentration flowing out from ξ₃Nono
Solution Lc₃Is the solution heat exchanger H on the high temperature side.₃Passing through the heating side of
After that, medium temperature regenerator G₂Solution on medium temperature side after flowing out from
Heat exchanger H₂Concentration passed through₂Concentrated solution Lc₂Meet with
Concentration ξ_mAnd return to absorber A as concentrated solution Lc of
Has become.

Further, in the present embodiment, the three waste heat heat exchangers K ₁ , K ₂ , K ₃ for heating the absorbing solution (dilute solution) Lw by the residual heat after heating the external heat source J. Is attached. These exhaust heat heat exchangers K ₁ , K ₂ and K ₃ are connected in parallel. The exhaust heat heat exchanger K ₃ is supposed to preheat the absorbing solution (dilute solution) Lw immediately before flowing into the high temperature regenerator G ₃ , and the exhaust heat heat exchanger K ₂ is the intermediate temperature regenerator G ₂
Is to preheat the absorbing solution (dilute solution) Lw immediately before flowing into the low temperature regenerator G ₁ and the exhaust heat heat exchanger K ₁ preheats the absorbing solution (dilute solution) Lw immediately before flowing into the low temperature regenerator G _1. It is said that.

By doing so, the regenerators G ₁ , G ₂ , G ₃
The absorbing solution (dilute solution) Lw flowing into the preheater is preheated by the residual heat after the heating of the external heat source J, so that the external heat source J can be effectively used and the regenerators G ₁ , G ₂ , G
The heating efficiency at ₃ is also improved.

[0115] The concentration xi] ₁ flowing from the low temperature regenerator G ₁
Absorption solution (concentrated solution) Lc ₁ is heated and boiled by the heat of the refrigerant vapor R ₃ generated in the high temperature regenerator G ₃ in the medium temperature regenerator G ₂ and further concentrated to an absorption solution (concentrated solution) of concentration ξ _2. L
It becomes c ₂ .

In this embodiment, three exhaust heat heat exchangers are used, but the high temperature regenerator G is used.
Absorbent solution immediately before flowing into the ₃ (dilute solution) Lw may also be a two and one of the exhaust heat exchanger K ₃ and another exhaust heat exchanger K _2, K ₁ for preheating the. Moreover, such an arrangement of the exhaust heat exchanger may be applied to other embodiments.

The other structure, function and effect are the same as those in the first embodiment, and the explanation thereof will be omitted.

Fourteenth Embodiment FIG. 26 shows a refrigeration cycle of an absorption refrigeration system according to a fourteenth embodiment of the present invention.

In this case, as compared with the thirteenth embodiment.
Is an exhaust heat exchanger K₁, K₂, K₃Are connected in series
The difference is only in the point that
The effect is the same as in the thirteenth embodiment, so the description will be omitted.
Omit it. In the present embodiment, three exhaust heats
A heat exchanger is used, but a high temperature regenerator G₃
Exhaust to preheat the absorbing solution (dilute solution) Lw just before flowing into the
Heat heat exchanger K₃And other waste heat exchanger K₂, K₁One of
It can also be two. Also, such exhaust heat
The arrangement of the heat exchanger may be applied to other embodiments.

Fifteenth Embodiment FIG. 27 shows a refrigeration cycle of an absorption refrigeration system according to a fifteenth embodiment of the present invention.

In this case, the same as in the fourth embodiment.
The refrigeration cycle is as follows, and it flowed out from the absorber A.
Concentration ξ_aAbsorption solution (dilute solution) Lw of the solution heat on the low temperature side
Exchanger H₁After passing through the heated side of the
One is the low temperature regenerator G₁The other side of the high temperature side
Solution heat exchanger H₃And the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, low temperature regeneration
Bowl G₁Outflow from ξ₁Concentrated solution Lc₁The solution pong
LP₂Solution heat exchanger H on the medium temperature side due to the pumping force of₂ Cover
Medium temperature regenerator G passing through the heating side₂Will flow into
ing. Also, the high temperature regenerator G₃Concentration flowing out from ξ₃Nono
Solution Lc₃Is the solution heat exchanger H on the high temperature side.₃Passing through the heating side of
After that, medium temperature regenerator G₂Solution on medium temperature side after flowing out from
Heat exchanger H₂Concentration passed through₂Concentrated solution Lc₂Meet with
Concentration ξ_mAnd return to absorber A as concentrated solution Lc of
Has become. By doing this, the low temperature regenerator G₁More flowing
Outgoing concentration ξ₁Absorption solution (concentrated solution) Lc₁But at medium temperature
Bowl G₂At high temperature regenerator G₃Refrigerant vapor R generated in₃of
It is heated and boiled by heat, further concentrated and the concentration ξ₂Absorption of
Liquid (concentrated solution) Lc₂Will be

Further, in this embodiment, the exhaust heat exchange is performed.
Immediately before the converter K, the absorption solution (dilute solution) Lw is branched.
After bypassing the exhaust heat exchanger K, the high temperature regenerator
G₃ I try to join them just before they flow into. this
By doing so, the flow rate of the solution flowing into the exhaust heat exchanger K becomes
Since it can be reduced, it is possible to reduce the size of the exhaust heat exchanger.
It

The form of such an exhaust heat exchanger is
It may be applied to other embodiments.

The other structure, function and effect are the same as those in the first embodiment, and the explanation thereof will be omitted.

Sixteenth Embodiment FIG. 28 shows a refrigerating cycle of an absorption type refrigerating apparatus according to a sixteenth embodiment of the present invention.

In this case, the same as in the fourth embodiment.
The refrigeration cycle is as follows, and it flowed out from the absorber A.
Concentration ξ_aAbsorption solution (dilute solution) Lw of the solution heat on the low temperature side
Exchanger H₁After passing through the heated side of the
One is the low temperature regenerator G₁The other side of the high temperature side
Solution heat exchanger H₃And the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, low temperature regeneration
Bowl G₁Outflow from ξ₁Concentrated solution Lc₁The solution pong
PL₂Solution heat exchanger H on the medium temperature side due to the pumping force of₂ Cover
Medium temperature regenerator G passing through the heating side₂Will flow into
ing. Also, the high temperature regenerator G₃Concentration flowing out from ξ₃Nono
Solution Lc₃Is the solution heat exchanger H on the high temperature side.₃Passing through the heating side of
After that, medium temperature regenerator G₂Solution on medium temperature side after flowing out from
Heat exchanger H₂Concentration passed through₂Concentrated solution Lc₂Meet with
Concentration ξ_mAnd return to absorber A as concentrated solution Lc of
Has become. By doing this, the low temperature regenerator G₁More flowing
Outgoing concentration ξ₁Absorption solution (concentrated solution) Lc₁But at medium temperature
Bowl G₂At high temperature regenerator G₃Refrigerant vapor R generated in₃of
It is heated and boiled by heat, further concentrated and the concentration ξ₂Absorption of
Liquid (concentrated solution) Lc₂Will be

In the present embodiment, the absorbing solution (dilute solution) L immediately before flowing into the solution heat exchanger H _3.
w is branched, one passes through the heated side of the solution heat exchanger H ₃ , the other passes through the heated side of the exhaust heat exchanger K, and then merges into the high temperature regenerator G _3. I have to. By doing so, the flow rate of the solution flowing into the exhaust heat heat exchanger K can be reduced, so that the exhaust heat heat exchanger can be downsized.

The form of such an exhaust heat exchanger is
It may be applied to other embodiments.

The other structure, functions and effects are the same as those in the first embodiment, and the explanation thereof is omitted.

Seventeenth Embodiment FIG. 29 shows a refrigerating cycle of an absorption refrigerating apparatus according to a seventeenth embodiment of the present invention.

In this case, the same as in the fourth embodiment.
The refrigeration cycle is as follows, and it flowed out from the absorber A.
Concentration ξ_aAbsorption solution (dilute solution) Lw of the solution heat on the low temperature side
Exchanger H₁After passing through the heated side of the
One is the low temperature regenerator G₁The other side of the high temperature side
Solution heat exchanger H₃And the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, low temperature regeneration
Bowl G₁Outflow from ξ₁Concentrated solution Lc₁The solution pong
PL₂Solution heat exchanger H on the medium temperature side due to the pumping force of₂ Cover
Medium temperature regenerator G passing through the heating side₂Will flow into
ing. Also, the high temperature regenerator G₃Concentration flowing out from ξ₃Nono
Solution Lc₃Is the solution heat exchanger H on the high temperature side.₃Passing through the heating side of
After that, medium temperature regenerator G₂Solution on medium temperature side after flowing out from
Heat exchanger H₂Concentration passed through₂Concentrated solution Lc₂Meet with
Concentration ξ_mAnd return to absorber A as concentrated solution Lc of
Has become. By doing this, the low temperature regenerator G₁More flowing
Outgoing concentration ξ₁Absorption solution (concentrated solution) Lc₁But at medium temperature
Bowl G₂At high temperature regenerator G₃Refrigerant vapor R generated in₃of
It is heated and boiled by heat, further concentrated and the concentration ξ₂Absorption of
Liquid (concentrated solution) Lc₂Will be

[0132] Further, in this embodiment, drain Rd ₂ flowing out of the intermediate temperature regenerator G ₂ is a drain heat exchanger D ₂
After passing through the heating side of the drain heat exchanger D ₁ , it joins the drain Rd ₁ flowing out from the low temperature regenerator G ₁ , and then passes through the heating side of the drain heat exchanger D ₁ and flows into the condenser C. By doing this, the drain R flowing out from the medium temperature regenerator G ₂
The heat possessed by d ₂ can be effectively used.

Such a form is also applicable to other embodiments.

The other structure, functions and effects are the same as those in the first embodiment, and the description thereof will be omitted.

18th Embodiment FIG. 30 shows a refrigerating cycle of an absorption refrigerating apparatus according to an 18th embodiment of the present invention.

In this case, the same as in the fourth embodiment.
The refrigeration cycle is as follows, and it flowed out from the absorber A.
Concentration ξ_aAbsorption solution (dilute solution) Lw of the solution heat on the low temperature side
Exchanger H₁After passing through the heated side of the
One is the low temperature regenerator G₁The other side of the high temperature side
Solution heat exchanger H₃And the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, low temperature regeneration
Bowl G₁Outflow from ξ₁Concentrated solution Lc₁The solution pong
LP₂Solution heat exchanger H on the medium temperature side due to the pumping force of₂ Cover
Medium temperature regenerator G that passed the heating side₂Will flow into
ing. Also, the high temperature regenerator G₃Concentration flowing out from ξ₃Nono
Solution Lc₃Is the solution heat exchanger H on the high temperature side.₃Passing through the heating side of
After that, medium temperature regenerator G₂Solution on medium temperature side after flowing out from
Heat exchanger H₂Concentration passed through₂Concentrated solution Lc₂Meet with
Concentration ξ_mAnd return to absorber A as concentrated solution Lc of
Has become. By doing this, the low temperature regenerator G₁More flowing
Outgoing concentration ξ₁Absorption solution (concentrated solution) Lc₁But at medium temperature
Bowl G₂At high temperature regenerator G₃Refrigerant vapor R generated in₃of
It is heated and boiled by heat, further concentrated and the concentration ξ₂Absorption of
Liquid (concentrated solution) Lc₂Will be

[0137] Further, in the present embodiment, after flowing out of the intermediate temperature regenerator G _2, and drain Rd ₂ which has passed through the heating side of the drain heat exchanger D _2, it is fed from the absorber A, a solution heat exchanger vessels H ₁ of inlet drain heat exchanger to drain Rd ₁ heat exchange with branched and flows out from the low temperature regenerator G ₁ in side D ₁
A drain heat exchanger D'is provided for exchanging heat with the absorbing solution (diluted solution) Lw that has passed through the heated side of. By doing so, the heat possessed by the drain Rd ₂ flowing out from the medium temperature regenerator G ₂ can be effectively utilized.

Such a form is also applicable to other embodiments.

The other structure, function and effect are the same as those in the first embodiment, and the description thereof will be omitted.

19th Embodiment FIG. 31 shows a refrigerating cycle of an absorption refrigerating apparatus according to a 19th embodiment of the present invention.

In this case, the same as in the fourth embodiment.
The refrigeration cycle is as follows, and it flowed out from the absorber A.
Concentration ξ_aAbsorption solution (dilute solution) Lw of the solution heat on the low temperature side
Exchanger H₁After passing through the heated side of the
One is the low temperature regenerator G₁The other side of the high temperature side
Solution heat exchanger H₃And the heated side of the exhaust heat exchanger K
High temperature regenerator G₃Is flowing into. Also, low temperature regeneration
Bowl G₁Outflow from ξ₁Concentrated solution Lc₁The solution pong
LP₂Solution heat exchanger H on the medium temperature side due to the pumping force of₂ Cover
Medium temperature regenerator G passing through the heating side₂Will flow into
ing. Also, the high temperature regenerator G₃Concentration flowing out from ξ₃Nono
Solution Lc₃Is the solution heat exchanger H on the medium temperature side.₂Passing through the heating side of
After that, medium temperature regenerator G₂After flowing out of
Heat exchanger H₂Concentration passed through₂Concentrated solution Lc₂Meet with
Concentration ξ_mAnd return to absorber A as concentrated solution Lc of
Has become. By doing this, the low temperature regenerator G₁More flowing
Outgoing concentration ξ₁Absorption solution (concentrated solution) Lc₁But at medium temperature
Bowl G₂At high temperature regenerator G₃Refrigerant vapor R generated in₃of
It is heated and boiled by heat, further concentrated and the concentration ξ₂Absorption of
Liquid (concentrated solution) Lc₂Will be

Further, in the present embodiment, it is fed from the absorber A and the drain Rd ₂ which flows out from the intermediate temperature regenerator G ₂ and is branched at the heating side inlet of the drain heat exchanger D ₂ .
Absorption solution (dilute solution) Lw that has branched on the inlet side of the solution heat exchanger H ₁ and has passed through the heated side of the drain heat exchanger D _{1 that} exchanges heat with the drain Rd ₁ flowing out from the low temperature regenerator G _1.
A drain heat exchanger D ″ for exchanging heat with and is attached.
In this way, the heat of the drain Rd ₂ flowing from the medium temperature regenerator G ₂ can be effectively used.

Such a form is also applicable to other embodiments.

The other structures, functions, and effects are the same as those in the first embodiment, and the description thereof will be omitted.

[0145]

According to the invention of claim 1, the condenser C, the absorber A, the evaporator E and the n (n ≧ 3) regenerators G ₁ to
G _n is a basic element, these elements are operatively connected by a solution pipe and a refrigerant pipe, and the regenerator G _n on the highest temperature side is heated and boiled by using an external heat source J such as fuel or steam. To generate the refrigerant vapor R _n , and heat the regenerator G _n-1 on the first-stage low temperature side using the heat of the refrigerant vapor R _n to generate the refrigerant vapor R _n.
n-1 is generated, further the refrigerant vapor R _n-1 further on the low temperature side regenerator using G _n-2 is heated to the refrigerant vapor R _n-2 most of the low-temperature side regenerator that generates a G _In the absorption refrigeration apparatus configured to be able to repeat up to _1, the absorption solution L after the refrigerant vapor generation in the regenerator _Gn on the highest temperature side
concentration xi] _n of c _n, the most low temperature side concentration absorption solution Lc ₁ after the occurrence refrigerant vapor in the regenerator G ₁ of xi] _1, wherein the concentration of the absorbent solution Lc flowing into the absorber A xi] _m, wherein When the concentration of the absorbing solution Lw flowing out from the absorber A is ξ _a ,
Since the refrigeration cycle is configured such that (ξ ₁ −ξ _a ) and (ξ _n −ξ _a ) are smaller than (ξ _m −ξ _a ), it is possible to reduce the temperature and pressure in the refrigeration cycle. Therefore, there is an effect that the cost can be reduced due to the reduction of the transportation power and the strength of each element constituting the refrigeration cycle, and the risk of corrosion can be reduced.

As in the invention of claim 2, claim 1
In the absorption refrigeration system described above, outflow from the absorber A
The absorbed solution Lw is branched, and one of
Regenerator G₁Flow into the
Part of the regenerator G with the highest temperature_n Configured to flow into
Regenerator G on the highest temperature side_nConcentration flowing into ξ_aSucking
The flow rate of the collecting solution (dilute solution) Lw can be reduced.
As a result, the sensible heat content of the heating and boiling absorbing solution Lw decreases. Servant
Therefore, the heat input to the regenerator is reduced, and COP
improves.

As in the invention of claim 3, claim 2
In the absorption refrigeration apparatus described, regeneration of the highest temperature side
Bowl G_nPart of the absorption solution Lw flowing into the
Regenerator G_nAnd the regenerator G at the lowest temperature side₁Provided between
Regenerator G on the medium temperature side₂~ G_n-1At least one or more of
When it is configured to flow into the₂ ~
G_n-1The flow rate of the solution flowing into the regenerator G on the highest temperature side_n
It is possible to reduce the flow rate to the regenerator on the medium temperature side.
G₂~ G_n-1Concentration of concentrated solution exiting₂~ Ξ_n-1Is the hottest side
Regenerator G_nConcentration of concentrated solution exiting_nGet bigger, contract
The effect of Requirement 1 can be easily obtained.

As in the invention of claim 4, claim 2
In the absorption refrigeration system according to any one of 1 and 3, the absorption solution Lc ₁ flowing out from the regenerator G ₁ on the lowest temperature side is the regenerator G _n on the highest temperature side and the regenerator G on the lowest temperature side. The regenerators G _{2 to} G _n-1 on the medium temperature side provided between the regenerators ₁ and _2.
If it is configured to flow into at least one of
The absorption solution (concentrated solution) Lc _{1 of} concentration ξ ₁ flowing out from the regenerator G ₁ on the lowest temperature side was generated in the regenerator G _n on the highest temperature side in the regenerators G _{2 to} G _n-1 on the medium temperature side. is heated to boiling by the heat of the refrigerant vapor R _n, further has a be concentrated, the concentration ξ ₂ ~ξ _n-1 is the lowest temperature side of the concentrated solution leaving the regenerator G ₂ ~G _n-1 of the medium-temperature side The concentration is larger than the concentration ξ ₁ of the concentrated solution exiting the regenerator G _{1 of the above,} and the effect in claim 1 can be easily obtained.

As in the invention of claim 5, claim 2
In the absorption refrigeration apparatus described, regeneration of the highest temperature side
Bowl G_nSolution Lc flowing out from the_nIs the hottest solution
Heat exchanger H_nThe medium temperature side with the next highest temperature after passing through the heating side of
Regenerator G_n-1Highest when configured to flow into
Regenerator G on the warm side_nConcentration flowing out from ξ_nAbsorption solution of (concentrated
Liquid) Lc_nThe heat held by the regenerator G at the highest temperature side_nTo
Concentration just before flowing in ξ_a Absorption solution (dilute solution) Lw
Will be accommodated (in other words, the regenerator on the highest temperature side)
G_nThe absorption solution (dilute solution) Lw flowing into the tank is preheated.
Therefore, the heat input from the external heat source J can be suppressed.
Wear.

As in the invention of claim 6, in the absorption refrigerating apparatus according to any one of claims 2, 3, 4 and 5, the total amount of the absorption solution Lw flowing out from the absorber A is the lowest. When configured to branch after passing through the heated side of the solution heat exchanger H _{1 on} the side, the absorbing solution Lw having the concentration ξ _a flowing out from the absorber A passes through the solution heat exchanger H ₁ on the lowest temperature side. The absorption solution (diluted solution) L, which is branched after being heated by heat recovery in the process, flows into the regenerator G _{1 on the} lowest temperature side and the regenerator G _n on the highest temperature side.
w will be preheated.

As in the invention of claim 7, in the absorption refrigerating apparatus according to any one of claims 2, 3, 4 and 5, the absorber A is provided on the solution outlet side of the absorber A.
A solution pump PL ₁ for pumping the absorbing solution Lw from the above is provided, and the absorbing solution Lw flowing out from the absorber A is provided.
However, when it is configured to branch immediately after the outlet of the solution pump PL ₁ , the absorbing solution (dilute solution) L having _a concentration of ξ _a
Immediately after the w has left the absorber A, the w is branched, and the inflow amount of the solution heat exchanger into which the branched absorption solution Lw flows is reduced, and the solution heat exchanger can be downsized.

As in the eighth aspect of the invention, in the absorption refrigeration system of any one of the second, third, fourth, fifth, sixth and seventh aspects, it flows into the regenerator G _n on the highest temperature side. The absorption solution Lw is the solution heat exchanger H _n on the highest temperature side.
Of the absorbing solution (dilute solution) L having _a concentration of ξ _a flowing into the regenerator G _n on the highest temperature side when it is configured to pass through the heated side of
Since w is preheated in the process of passing through the solution heat exchanger H _n on the highest temperature side, the amount of heat input from the external heat source J can be suppressed.

As in the invention of claim 9, claim
Absorption according to any one of 2, 3, 4, 5, 6 and 7.
Type refrigerating apparatus, the regenerator G on the lowest temperature side₁Flow
The absorption solution Lw to be introduced is the solution heat exchanger H on the lowest temperature side.₁
Of the regenerator G on the highest temperature side while passing through the heated side of
_nThe absorption solution Lw flowing into the is the solution heat on the lowest temperature side.
Exchanger H₁Solution heat exchanger H on the 1st stage higher temperature side₂Highest from
Solution heat exchanger H on warm side_n Solution heat exchanger up to H₂~ H_nof
When configured to pass through the heated side, the lowest temperature side
Regenerator G₁Concentration flowing into ξ_aAbsorption solution (dilute solution) Lw
Is the solution heat exchanger H on the lowest temperature side₁In the process of passing through
While being heated, the regenerator G on the highest temperature side_nConcentration flowing into
ξ_aAbsorption solution (dilute solution) Lw is the solution heat on the lowest temperature side.
Exchanger H₁Solution heat exchanger H on the 1st stage higher temperature side₂Highest from
Solution heat exchanger H on warm side_nSolution heat exchanger up to H₂~ H_nTo
It will be preheated in the process of passing through the regenerator G.₁, G_n
The thermal efficiency in is improved.

[0154] As in the invention of claim 10, claim
Any one of 2, 3, 4, 5, 6, 7, 8 and 9
In the absorption refrigeration equipment listed above, the highest
Regenerator G on the warm side_nAnd the regenerator G on the lowest temperature side₁Playback except
Bowl G₂~ G_n-1The absorbing solution that has flowed into the chamber is heated and becomes a refrigerant vapor.
R₂~ R_n-1To generate the respective concentration ξ₂~ Ξn_-1Concentrated
Liquid Lc₂~ Lc_n-1And each regenerator G₂~ G_n-1Outflow
And other regenerator G_n , G₁Solution Lc flowing out from
_n, Lc₁Confluence with the concentration ξ_mBefore becoming the absorption solution Lc of
When it is configured to flow into the absorber A,
Regenerator G on the hottest side_nAnd the regenerator G on the lowest temperature side₁And
Excluding regenerator G₂~ G_n-1The absorption solution flowing into the
Refrigerant vapor R₂~ R_n-1Generated and concentrated,
Degree ξ₂~ Ξn_-1Concentrated solution Lc₂~ Lc_n-1Become each play
Bowl G₂~ G_n-1Spills other regenerator G₁, G_nFlow from
Absorbed solution Lc_n, Lc₁Confluence with the concentration ξ_mAbsorption of
The solution Lc is returned to the absorber A, and the highest temperature
Side regenerator G_nAnd the regenerator G on the lowest temperature side₁Regenerator excluding and
G₂~ G_n-1In this way, efficient solution concentration can be performed.
Wear.

As in the invention of claim 11, in the absorption type refrigerating apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9 and 10, the absorber A is used.
When the evaporator E is divided into a plurality of stages having different refrigerant evaporation temperatures, the one having a higher refrigerant evaporation temperature (that is, the higher pressure stage) has a lower concentration, and therefore the cycle can be shifted to a thinner one.

As in the invention of claim 12, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10 and 11
In the absorption refrigerating apparatus according to any one of items 1 to 5, when the regenerator G ₁ and the condenser C on the lowest temperature side are divided into a plurality of stages having different refrigerant condensation temperatures, one having a lower refrigerant evaporation temperature (that is, a lower pressure stage). ), The operating pressure can be reduced because the pressure is reduced.

As in the invention of claim 13, in the absorption refrigerating apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11 and 12,
When the path of the absorbing solution is heated at least at one or more places by the residual heat after the heating of the external heat source J that heats the regenerator G _n on the highest temperature side, the residual heat after the heating of the external heat source J is used. The absorption solution will be heated,
The external heat source J can be effectively used. Case, and that the absorption solution is heated regenerator G ₁ ~G _n-1, except for the regenerator G _n of highest temperature side by steam drain Rd ₁ ~Rd _n-1 after heating, steam drain Rd ₁ ~ Rd _The heat of _n-1 can be effectively used.

According to the fifteenth aspect of the invention, in the absorption refrigerating apparatus according to the fourteenth aspect, the solution heat exchangers H _{1 to} H _n-1 other than the highest temperature side solution heat exchanger H _n are to be heated. immediately before the side inlet branches the part of the absorbent solution, the highest temperature side of the regenerator the steam drain Rd ₁ ~ Rd after heating the regenerator G ₁ ~G _n-1, except for G _n in the branch path
_n-1 is used to heat the absorbing solution and then the solution heat exchanger H ₁
When configured to merge at the heated side outlet of to H _n-1, the regenerator G ₁ ~G except regenerator G _n of highest temperature side
Some of the absorbent solution Lw branched immediately before the heated side inlet of the _n-1 steam drain Rd ₁ after heating the ~Rd solution heat exchanger by _n-1 H ₁ to H _{n -1} is heated, after which the solution The heat exchangers H _{1 to} H _n-1 are joined at the heated side outlets, and the heat held by the steam drains Rd _{1 to} Rd _n-1 can be effectively used.

As in the invention of claim 16, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 1
In the absorption refrigeration apparatus according to any one of 2, 13, 14 and 15, the temperature difference between the inlet side temperature and the outlet side temperature of the cold water We obtained in the evaporator E is 6 ° C or more. In this case, the flow rate of the cold water We can be reduced to reduce the transport power, the refrigerant evaporation temperature can be increased, and the cycle can be shifted to the thinner side.

As in the invention of claim 17, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 1
The absorption refrigeration apparatus according to any one of 2, 13, 14, 15 and 16, wherein the condenser C and the absorber A are provided.
When the cooling water Wa that cools the cooling water is configured to flow from the condenser C to the absorber A, the pressure of the condenser C can be lowered, so that the temperature and pressure of the refrigeration cycle can be easily lowered.

As in the invention of claim 17, claims 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 11, 1
In the absorption refrigerating apparatus according to any one of 2, 13, 14, 15, 16 and 17, when n = 3, the temperature and pressure of the high temperature side regenerator G ₃ can be suppressed.

[Brief description of drawings]

FIG. 1 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to a first embodiment of the present invention.

FIG. 2 is a Dühring diagram showing a state change of the absorbing solution in the absorption refrigerating apparatus according to the first embodiment of the present invention.

FIG. 3 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to a second embodiment of the present invention.

FIG. 4 is a Duhring diagram showing a state change of the absorbing solution in the absorption refrigerating apparatus according to the second embodiment of the present invention.

FIG. 5 is a refrigeration cycle diagram of an absorption refrigeration system according to a third embodiment of the present invention.

FIG. 6 is a Dühring diagram showing the state change of the absorbing solution in the absorption refrigerating apparatus according to the third embodiment of the present invention.

FIG. 7 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to a fourth embodiment of the present invention.

[Fig. 8] Fig. 8 is a Duhring diagram showing a state change of the absorbing solution in the absorption refrigerating apparatus according to the fourth embodiment of the present invention.

FIG. 9 is a refrigeration cycle diagram of an absorption refrigeration system according to a fifth embodiment of the present invention.

FIG. 10 is a Dühring diagram showing the state change of the absorbing solution in the absorption refrigerating apparatus according to the fifth embodiment of the present invention.

FIG. 11 is a refrigeration cycle diagram of an absorption refrigeration system according to a sixth embodiment of the present invention.

FIG. 12 is a Duhring diagram showing a state change of the absorbing solution in the absorption refrigerating apparatus according to the sixth embodiment of the present invention.

FIG. 13 is a refrigeration cycle diagram of an absorption refrigeration system according to a seventh embodiment of the present invention.

FIG. 14 is a Duhring diagram showing a change in the state of the absorbing solution in the absorption refrigerating apparatus according to the seventh embodiment of the present invention.

FIG. 15 is a refrigerating cycle diagram of an absorption refrigerating apparatus according to an eighth embodiment of the present invention.

FIG. 16 is a Dühring diagram showing the state change of the absorbing solution in the absorption refrigerating apparatus according to the eighth embodiment of the present invention.

FIG. 17 is a refrigerating cycle diagram of an absorption refrigerating apparatus according to a ninth embodiment of the present invention.

FIG. 18 is a Duhring diagram showing a state change of the absorbing solution in the absorption refrigerating apparatus according to the tenth embodiment of the present invention.

FIG. 19 is a refrigeration cycle diagram of an absorption refrigeration system according to an eleventh embodiment of the present invention.

[Fig. 20] Fig. 20 is a Duhring diagram showing the state change of the absorbing solution in the absorption refrigerating apparatus according to the eleventh embodiment of the present invention.

FIG. 21 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to a twelfth embodiment of the present invention.

FIG. 22 is a Duhring diagram showing a change in state of the absorbing solution in the absorption refrigerating apparatus according to the twelfth embodiment of the present invention.

FIG. 23 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to a thirteenth embodiment of the present invention.

FIG. 24 is a Dühring diagram showing a change in state of the absorbing solution in the absorption refrigerating apparatus according to the thirteenth embodiment of the present invention.

FIG. 25 is a refrigeration cycle diagram of an absorption type refrigeration system according to a fourteenth embodiment of the present invention.

FIG. 26 is a refrigeration cycle diagram of an absorption type refrigeration system according to a fifteenth embodiment of the present invention.

FIG. 27 is a refrigerating cycle diagram of the absorption refrigerating apparatus according to the sixteenth embodiment of the present invention.

FIG. 28 is a refrigerating cycle diagram of the absorption type refrigerating apparatus according to the seventeenth embodiment of the present invention.

FIG. 29 is a refrigerating cycle diagram of the absorption refrigerating apparatus according to the eighteenth embodiment of the present invention.

FIG. 30 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to a nineteenth embodiment of the present invention.

FIG. 31 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to a twentieth embodiment of the present invention.

FIG. 32 is a refrigeration cycle diagram of an absorption refrigeration system according to Conventional Example 1.

FIG. 33 is a refrigeration cycle diagram of an absorption refrigeration apparatus according to Conventional Example 2.

FIG. 34 is a refrigeration cycle diagram of an absorption refrigeration system according to Conventional Example 3.

FIG. 35 is a Dühring diagram showing a state change of the absorbing solution in the absorption refrigerating apparatus according to Conventional Example 1.

FIG. 36 is a Dühring diagram showing the state change of the absorbing solution in the absorption refrigerating apparatus according to Conventional Example 2.

FIG. 37 is a Dühring diagram showing a change in state of the absorbing solution in the absorption refrigerating device according to Conventional Example 3.

[Explanation of symbols]

A is an absorber, C is a condenser, D is a drain heat exchanger, E is an evaporator, G is a regenerator, H is a solution heat exchanger, J is an external heat source,
K is an exhaust heat exchanger, Lc is an absorbing solution (concentrated solution), Lw is an absorbing solution (dilute solution), PL is a solution pump, R is a refrigerant vapor, Rd is a drain vapor, and ξ is a concentration.

   ─────────────────────────────────────────────────── ─── Continued front page    F-term (reference) 3L093 BB11 BB12 BB13 BB14 BB16                       BB37 MM02 MM07

Claims (18)

[Claims] 1. A condenser (C), an absorber (A), an evaporator (E) and n (n ≧ 3) regenerators (G ₁ ) to (G _n ) are used as basic elements, and these elements are used. Are operatively connected by a solution pipe and a refrigerant pipe, and the regenerator ( _Gn ) on the highest temperature side is heated and boiled by using an external heat source (J) such as fuel or steam to make the refrigerant vapor (Rn _). ) Is generated and the heat of the refrigerant vapor (R _n ) is used to heat the regenerator (G _n-1 ) on the first-stage low temperature side to generate the refrigerant vapor (R _n-1 ). (R _n-1 ), and a regenerator (G _n-2 ) on the lower temperature side is used.
An absorption type refrigerating apparatus configured to be able to repeatedly heat a refrigerant to generate a refrigerant vapor (R _n-2 ) up to the coolest side regenerator (G ₁ ), wherein the highest temperature side regenerator The concentration of the absorbing solution (Lc _n ) after the refrigerant vapor generation in (G _n ) is ξ _n , and the concentration of the absorbing solution (Lc ₁ ) after the refrigerant vapor generation in the regenerator (G ₁ ) on the lowest temperature side is ξ ₁ , The concentration of the absorbing solution (Lc) flowing into the absorber (A) is ξ _m ,
When the concentration of the absorbing solution (Lw) flowing out from the absorber (A) is ξ _a , (ξ ₁ −ξ _a ) and (ξ _n −ξ _a ) are smaller than (ξ _m −ξ _a ). An absorption type refrigerating apparatus having a refrigeration cycle configured as described above. 2. The absorption solution (Lw) flowing out from the absorber (A) is branched, one is flown into the regenerator (G ₁ ) at the lowest temperature side, and the other is the total amount or one of the branched amounts. The absorption refrigerating apparatus according to claim 1, wherein a part is configured to flow into the regenerator ( _Gn ) on the highest temperature side. 3. A part of the absorption solution (Lw) flowing into the hottest regenerator (G _n ) is a part of the hottest regenerator (G _n ) and the coldest regenerator (G _n ). ₁₎ and the intermediate temperature side of the regenerator provided between the _{(G 2) ~ (G n} -1) of claim 2 absorption type, wherein a configured to flow into the at least one Refrigeration equipment. 4. The absorption solution (Lc ₁ ) flowing out from the regenerator (G ₁ ) on the lowest temperature side is the regenerator (G _n ) on the highest temperature side and the regenerator (G ₁ ) on the lowest temperature side. The regenerators (G ₂ ) to (G _n-1 ) on the intermediate temperature side provided between the first and _second sides are configured to flow into at least one or more of the regenerators (G ₂ ) to (G _n-1 ). The absorption type refrigerating apparatus according to the item. 5. The absorption solution (Lc _n ) flowing out of the regenerator (G _n ) on the highest temperature side passes through the heating side of the solution heat exchanger (H _n ) on the highest temperature side and then reaches the one-stage low temperature side. Regenerator (G
The absorption type refrigerating apparatus according to claim 2, wherein the absorption refrigerating apparatus is configured to flow into ( _n-1 ). 6. The total amount of the absorption solution (Lw) flowing out from the absorber (A) is the solution heat exchanger (H ₁ ) at the lowest temperature side.
The absorption type refrigerating apparatus according to any one of claims 2, 3, 4 and 5, wherein the absorption type refrigerating apparatus is configured to branch after passing through a heated side of the. 7. A solution pump (PL ₁ ) for pumping the absorbing solution (Lw) from the absorber (A) is provided on the solution outlet side of the absorber (A), and the absorber (A) is also provided. The absorption solution (Lw) flowing out from the solution pump (PL)
The absorption type refrigerating apparatus according to any one of claims 2, 3, 4 and 5, wherein the absorption refrigerating apparatus is configured to branch immediately after the exit of ₁ ). 8. The absorption solution (Lw) flowing into the highest temperature side regenerator (G _n ) is configured to pass through the heated side of the highest temperature side solution heat exchanger (H _n ). The absorption type refrigerating apparatus according to any one of claims 2, 3, 4, 5, 6 and 7, characterized in that. 9. The absorption solution (Lw) flowing into the regenerator (G ₁ ) on the lowest temperature side passes through the heated side of the solution heat exchanger (H ₁ ) on the lowest temperature side while side of regenerator absorbent solution flowing into (G _n) (Lw) is the most cold side solution heat exchanger (H ₁₎ from one step high-temperature side of the solution heat exchanger (H ₂₎ from the highest temperature side solution heat exchanger (H _n)
3. The solution heat exchangers (H ₂ ) to (H _n ) up to the heated side are passed through.
The absorption type refrigerating apparatus according to any one of 3, 4, 5, 6 and 7. 10. Regenerators (G ₂ ) to (G _n-1 ) excluding the regenerator on the highest temperature side (G _n ) and the regenerator on the lowest temperature side (G ₁ ) of the regenerators. The absorbing solution is heated to generate refrigerant vapors (R ₂ ) to (R _n-1 ), each of which has a concentration (ξ
₂₎ ~ _{(ξn - 1)} of the concentrated solution _{(Lc 2) ~ (Lc n} -1) and turned with the regenerator (G ₂₎ flows - a (G _n-1), other regenerator (G _n ), (G ₁ ) flowing out the absorbing solution (L
c _n), (the claim, characterized by being configured as Lc ₁₎ merging to a concentration (absorption solution xi] _m) (Lc) and to flow into the absorber (A) 2,3 4, 5,
The absorption refrigerating apparatus according to any one of 6, 7, 8 and 9. 11. The absorber (A) and evaporator (E).
The absorption refrigerating apparatus according to any one of claims 1, 2, 3, 4, 5, 6, 7, 8, 9 and 10, wherein the refrigerant is divided into a plurality of stages having different refrigerant evaporation temperatures. 12. The coldest regenerator (G ₁ ) and the condenser (C) are divided into a plurality of stages having different refrigerant condensation temperatures. ,
The absorption refrigeration apparatus according to any one of 6, 7, 8, 9, 10 and 11. 13. The absorption solution path is configured to be heated at least at one or more places by the residual heat after the heating of the external heat source (J) for heating the regenerator (G _n ) on the highest temperature side. Said claim 1, 2, 3, 4, 5,
13. The absorption refrigerating apparatus according to any one of 6, 7, 8, 9, 10, 11 and 12. 14. The steam drains (Rd ₁ ) to (Rd _n-1 ) after heating the regenerators (G ₁ ) to (G _n-1 ) excluding the regenerator (G _n ) on the highest temperature side. The above-mentioned claim 1 or 2, characterized in that at least one or more of the paths of the absorbing solution are configured to be heated at at least one or more locations.
The absorption refrigerating apparatus according to any one of 3, 4, 5, 6, 7, 8, 9, 10, 11, 12 and 13. 15. A part of the absorbing solution is branched immediately before the heated side inlets of the solution heat exchangers (H ₁ ) to (H _n-1 ) excluding the solution heat exchanger (H _n ) on the highest temperature side. In the branch path, the steam drains (Rd ₁ ) to (Rd _n-1 ) after heating the regenerators (G ₁ ) to (G _n-1 ) excluding the regenerator (G _n ) on the highest temperature side 15. The absorption formula according to claim 14, characterized in that the absorption solution is heated by using, and then merged at the heated side outlets of the solution heat exchangers (H ₁ ) to (H _n-1 ). Refrigeration equipment. 16. The temperature difference between the inlet side temperature and the outlet side temperature of the cold water We obtained in the evaporator E is 6 ° C. or more, and the temperature difference is 6 ° C. or more.
3, 4, 5, 6, 7, 8, 9, 10, 11, 12, 1
The absorption refrigerating apparatus according to any one of 3, 14, and 15. 17. The condenser (C) and the absorber (A).
The cooling water (Wa) for cooling the cooling water (Wa) is configured to flow from the condenser (C) to the absorber (A). , 8, 9, 1
The absorption type refrigerating apparatus according to any one of 0, 11, 12, 13, 14, 15 and 16. 18. The method of claim 1, 2, 3, 4, 5, 6, 7, 8, 9, 10, 1 wherein n = 3.
18. The absorption refrigeration system according to any one of 1, 12, 13, 14, 15, 16 and 17.